Methods and systems of upgrading heavy aromatics stream to petrochemical feedstock

ABSTRACT

Provided here are systems and methods that integrate a hydrodearylation process and a transalkylation process into an aromatic recovery complex. Various other embodiments may be disclosed and claimed.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a continuation-in-part application of U.S. application Ser. No. 16/388,563, filed Apr. 18, 2019, which itself is a continuation-in-part application of U.S. application Ser. No. 16/032,642, filed on Jul. 11, 2018 and issued as U.S. Pat. No. 10,294,172 on May 21, 2019, which is a continuation application of U.S. application Ser. No. 15/435,039, filed on Feb. 16, 2017 and issued as U.S. Pat. No. 10,053,401 on Aug. 21, 2018.

TECHNICAL FIELD

The disclosure relates to methods and systems of upgrading heavy aromatics stream to petrochemical feedstock, and more specifically to a combination of a hydrodearylation unit and a transalkylation unit in an aromatics recovery complex.

BACKGROUND

In an aromatics complex, a variety of process units are used to convert naphtha or pyrolysis gasoline into benzene, toluene and mixed xylenes, which are basic petrochemical intermediates used for the production of various other chemical products. In order to maximize the production of benzene, toluene and mixed xylenes, the feed to an aromatics complex is generally limited from C₆ up to C₁₁ compounds. In most aromatic complexes, the mixed xylenes are processed within the complex to produce the particular isomer-para-xylene, which can be processed downstream to produce terephthalic acid. This terephthalic acid is used to make polyesters, such as polyethylene terephthalate. In order to increase the production of benzene and para-xylene, the toluene and C₉ and C₁₀ aromatics are processed within the complex through a toluene, C₉, C₁₀ transalkylation/toluene disproportionation (TA/TDP) process unit to produce benzene and xylenes. Any remaining toluene, C₉, and C₁₀ aromatics are recycled to extinction. Compounds heavier than C₁₀ are generally not processed in the TA/TDP unit, as they tend to cause rapid deactivation of the catalysts used at the higher temperatures used in these units, often greater than 400° C.

When para-xylene is recovered from mixed xylenes by a selective adsorption process unit in the complex, the C₈ feed to the selective adsorption unit is processed to eliminate olefins and alkenyl aromatics such as styrene in the feed. Olefinic material can react and occlude the pores of the zeolite adsorbent. The olefinic material is removed by passing a C₈₊ stream across a clay or acidic catalyst to react olefins and alkenyl aromatics with another (typically aromatic) molecule, forming heavier compounds (C₁₆₊). These heavier compounds are typically removed from the mixed xylenes by fractionation. The heavy compounds cannot be processed in the TA/TDP unit due to their tendency to deactivate the catalyst and are generally removed from the complex as lower value fuels blend stock. As many of the heavy alkyl aromatic compounds fractionate with the fractions containing greater than 10 carbon atoms, they are not typically sent as feedstock to the transalkylation unit, and instead are sent to gasoline blending or used as fuel oil.

SUMMARY

A need has been recognized for the characterization and recovery of higher value light aromatics in the range from C₆ to C₁₀ from certain heavy compounds before processing aromatic streams through specialized product production units, such as the TA/TDP unit. Embodiments disclosed here include characterization of the products formed during the treatment of aromatics streams during processing of hydrocarbons. Certain embodiments include processes for recovery of alkyl mono-aromatic compounds. An embodiment of the process for recovery of alkyl mono-aromatic compounds includes the steps of (a) supplying a feed stream containing C₉₊ compounds from an aromatic complex to a separator to produce a first product stream containing C₉ and C₁₀ compounds and a second product stream containing one or more of heavy alkyl aromatic compounds and alkyl-bridged non-condensed alkyl multi-aromatic compounds; (b) supplying the first product stream containing C₉ and C₁₀ compounds to a transalkylation/toluene disproportionation process unit to yield a third product stream enriched in C₈ compounds; (c) allowing a hydrogen stream and the second product stream to react in presence of a catalyst under specific reaction conditions in a hydrodearylation reactor to yield a fourth product stream containing one or more alkyl mono-aromatic compounds and a fifth product stream containing C₁₁₊ compounds; and (d) supplying the fourth product stream to the toluene transalkylation/toluene disproportionation process unit to produce alkyl mono-aromatic compounds. In an embodiment, the fourth product stream and the first product stream containing C₉ and C₁₀ compounds are mixed to form a feed stream for the toluene transalkylation/toluene disproportionation process unit. The feed stream can be from a xylene rerun column of an aromatic recovery process. The feed stream can be undiluted by a solvent. A portion of the hydrogen stream may be supplied to a catalyst bed in the hydrodearylation reactor to quench the catalyst bed. The process can further include supplying the fourth product stream containing one or more alkyl mono-aromatic compounds to a separator to recover a benzene-containing stream; and supplying the benzene-containing stream to the toluene transalkylation/toluene disproportionation process unit to produce alkyl mono-aromatic compounds. The process can further include recovering a C₈ stream from the separator; and supplying the C₈ stream to a para-xylene unit to produce para-xylene. The process can further include recovering a C₉₊ stream from the separator; and supplying the C₉₊ stream to the toluene transalkylation/toluene disproportionation process unit to produce alkyl mono-aromatic compounds. The process can further include supplying the fourth product stream containing one or more alkyl mono-aromatic compounds to a separator to recover a toluene-containing stream; and supplying the toluene-containing stream to the toluene transalkylation/toluene disproportionation process unit to produce alkyl mono-aromatic compounds.

The catalyst in the hydrodearylation reactor can include a support made of one or more of silica, alumina, titania, and a combination thereof. The catalyst in the hydrodearylation reactor can further include an acidic component being at least one member of the group consisting of amorphous silica-alumina, zeolite, and combinations thereof. The zeolite can be one or more of or derived from FAU, *BEA, MOR, MFI, or MWW framework types, wherein each of these codes correspond to a zeolite structure present in the database of zeolite structures as maintained by the Structure Commission of the International Zeolite Association. The catalyst in the hydrodearylation reactor can include an IUPAC Group 6-10 metal that is at least one member of the group consisting of iron, cobalt, nickel, molybdenum, tungsten, and combinations thereof. The IUPAC Group 8-10 metal can be present ranging from 2 to 20 percent by weight of the catalyst and the IUPAC Group 6 metal can be present ranging from 1 to 25 percent by weight of the catalyst. The conditions in the hydrodearylation reactor can include an operating temperature in the range of about 200 to 450° C., or about 250 to 450° C. and an operating hydrogen partial pressure in the range of about 5 bar gauge to 100 bar gauge. One of the alkyl mono-aromatic compounds produced by the toluene transalkylation/toluene disproportionation is a para-xylene.

Certain embodiments include systems for recovery of alkyl mono-aromatic compounds. An embodiment of a system for conversion of alkyl-bridged non-condensed alkyl multi-aromatic compounds to alkyl mono-aromatic compounds includes the following components: (i) a first separator adapted to receive a feed stream containing one or more of heavy alkyl aromatic compounds and one or more alkyl-bridged non-condensed alkyl multi-aromatic compounds having at least two benzene rings connected by an alkyl bridge group with at least two carbons and the benzene rings being connected to different carbons of the alkyl bridge group, and produces a first product stream containing C₉ and C₁₀ compounds and a second product stream containing one or more of heavy alkyl aromatic compounds and alkyl-bridged non-condensed alkyl multi-aromatic compounds; (ii) a hydrodearylation reactor fluidly coupled to the first separator and adapted to receive a hydrogen stream and the second product stream and to produce a third product stream in presence of a catalyst, the third product stream containing one or more alkyl mono-aromatic compounds; and (iii) a second separator fluidly coupled to the hydrodearylation reactor and adapted to receive the third product stream and to produce a benzene-containing stream, a toluene-containing stream, a C₈-rich stream, and a bottoms C₉₊ stream. The system can also include a transalkylation unit fluidly coupled to the second separator and adapted to receive the first product stream and one or more of the benzene-containing stream, the toluene-containing stream, and the bottoms C₉₊ stream, and to produce alkyl mono-aromatic compounds. The system can also include a para-xylene unit fluidly coupled to the second separator and adapted to receive the C₈-rich stream and to produce a para-xylene-rich stream.

BRIEF DESCRIPTION OF THE DRAWINGS

Embodiments will be readily understood by the following detailed description in conjunction with the accompanying drawings. Embodiments are illustrated by way of example and not by way of limitation in accompanying drawings.

FIG. 1 is a schematic representation of certain components of an aromatics processing system that upgrades fuel oil to a petrochemical feedstock, according to an exemplary embodiment.

FIG. 2 is a schematic representation of certain components of an aromatics processing system that upgrades fuel oil to a petrochemical feedstock, according to an exemplary embodiment.

FIG. 3 is a schematic representation of certain components of an aromatics processing system that upgrades fuel oil to a petrochemical feedstock, according to an exemplary embodiment.

FIG. 4 is a schematic representation of certain components of an aromatics processing system that upgrades fuel oil to a petrochemical feedstock, according to an exemplary embodiment.

FIG. 5 is a schematic representation of certain components of an aromatics processing system that upgrades fuel oil to a petrochemical feedstock, according to an exemplary embodiment.

DETAILED DESCRIPTION

The present disclosure describes various embodiments related to processes, devices, and systems for conversion of alkyl-bridged non-condensed alkyl aromatic compounds to alkyl mono-aromatic compounds. Further embodiments are described and disclosed.

In the following description, numerous details are set forth in order to provide a thorough understanding of the various embodiments. In other instances, well-known processes, devices, and systems may not have been described in particular detail in order not to unnecessarily obscure the various embodiments. Additionally, illustrations of the various embodiments may omit certain features or details in order to not obscure the various embodiments. Here, reference is made to the accompanying drawings that form a part of this disclosure. The drawings may provide an illustration of some of the various embodiments in which the subject matter of the present disclosure may be practiced. Other embodiments may be utilized, and logical changes may be made without departing from the scope of this disclosure. Therefore, the following detailed description is not to be taken in a limiting sense.

The description may use the phrases “in some embodiments,” “in various embodiments,” “in an embodiment,” or “in embodiments,” which may each refer to one or more of the same or different embodiments. Furthermore, the terms “comprising,” “including,” “having,” and the like, as used with respect to embodiments of the present disclosure, are synonymous.

As used in this disclosure, the term “hydrodearylation” refers to a process for cleaving of the alkyl bridge of non-condensed alkyl-bridged multi-aromatics or heavy alkyl aromatic compounds to form alkyl mono-aromatics, in the presence a catalyst and hydrogen.

As used in this disclosure, the term “stream” (and variations of this term, such as hydrocarbon stream, feed stream, product stream, and the like) may include one or more of various hydrocarbon compounds, such as straight chain, branched or cyclical alkanes, alkenes, alkadienes, alkynes, alkyl aromatics, alkenyl aromatics, condensed and non-condensed di-, tri- and tetra-aromatics, and gases such as hydrogen and methane, C₂₊ hydrocarbons and further may include various impurities.

As used in this disclosure, the term “zone” refers to an area including one or more equipment, or one or more sub-zones. Equipment may include one or more reactors or reactor vessels, heaters, heat exchangers, pipes, pumps, compressors, and controllers. Additionally, an equipment, such as reactor, dryer, or vessels, further may include one or more zones.

As used in this disclosure, the term “rich” means an amount of at least 30% or greater, by mole percentage of a compound or class of compounds in a stream. Certain streams rich in a compound or class of compounds can contain about 50% or greater, by mole percentage of the particular compound or class of compounds in the streams. In certain cases, mole percentage may be replaced by weight percentage, in accordance with standard industry usage.

As used in this disclosure, the term “mixed xylenes” refers to a mixture containing one or more C₈ aromatics, including any one of the three isomers of di-methylbenzene and ethylbenzene. As used in this disclosure, the term “conversion” refers to the conversion of compounds containing multiple aromatic rings or mono-aromatic compounds with heavy (C4+) alkyl groups boiling above 210° C. to mono-aromatic compounds with a lighter alkyl groups boiling below 210° C.

During hydrocarbon processing, compounds composed of an aromatic ring with one or more coupled alkyl groups containing three or more carbon molecules per alkyl group are formed. Formation of these compounds may be from processes used by petroleum refiners and petrochemical producers to produce aromatic compounds from non-aromatic hydrocarbons, such as catalytic reforming. As many of these heavy alkyl aromatic compounds fractionate with the fractions containing greater than 10 carbon atoms, they are not typically sent as feedstock to the transalkylation unit, and instead are sent to gasoline blending or used as fuel oil. The methods and systems disclosed here result in upgrading a low-value fuel oil to petrochemical feed.

Provided here is an embodiment of a process to fractionate an effluent stream of a xylene re-run column and supply it as a feed stream to a hydrodearylation unit. In an embodiment, this stream is either subsequently processed or used to upgrade the fuel oil components (heavy fraction) to petrochemical feedstock. Methods and system disclosed here create value by processing a reject/bottoms stream from an aromatic complex and by upgrading a significant proportion of fuel oil into petrochemical feedstock. In an embodiment, the C₉₊ stream from a xylene re-run column is fractionated to remove C₉ and C₁₀, leaving a C₁₁₊ stream, which is considered as a low-value fuel oil stream. The C₉ and C₁₀ stream is directed to a TA/TDP process unit to yield increased quantities of C₈ that can be further processed downstream to yield para-xylene. The C₁₁₊ fuel oil stream is subjected to hydrodearylation and the hydrodearylated liquid products sent for processing in a transalkylation unit. The unconverted C₁₁₊ (mainly condensed diaromatics) stream is directed as fuel oil.

Disclosed here is a process for recovery of alkyl mono-aromatic compounds that includes the following steps. A feed stream containing C₉₊ compounds from an aromatic complex is supplied to a separator to produce a first product stream containing C₉ and C₁₀ compounds and a second product stream containing one or more of heavy alkyl aromatic compounds and alkyl-bridged non-condensed alkyl multi-aromatic compounds. In an embodiment, the feed stream is from a xylene rerun column of an aromatic recovery process. In certain embodiments, the feed stream is undiluted by solvents and is directly supplied to the separator. In an embodiment, the second product stream contains C₁₁₊ compounds. This first product stream containing C₉ and C₁₀ compounds is supplied to a TA/TDP process unit to yield a third product stream enriched in C₈ compounds. The second product stream and a hydrogen stream are supplied to a hydrodearylation reactor to react in presence of a catalyst under specific reaction conditions to yield a fourth product stream containing C₉ and C₁₀ compounds and a fifth product stream containing unconverted C₁₁₊ compounds. The fourth product stream is supplied further to a TA/TDP process unit to supply and produce alkyl mono-aromatic compounds. In certain embodiments, the C₈ content in the fourth product stream increases following the processing in the TA/TDP process unit. In certain embodiments, the fifth product stream containing unconverted C₁₁₊ compounds can be recycled to the hydrodearylation reactor. In certain embodiments, the fourth product stream and the first product stream containing C9 and C10 compounds are mixed to form a feed stream for the TA/TDP process unit. In certain embodiments, the alkyl mono-aromatic compounds produced by the TA/TDP process unit is para-xylene. In certain embodiments, the hydrodearylated products are supplied to a separator to recover a benzene-containing stream. And this benzene-containing stream can be directed to an appropriate part of the TA/TPD process unit. In certain embodiments, the hydrodearylated products are supplied to a separator to recover a toluene-containing stream. And this toluene-containing stream can be directed to an appropriate part of the TA/TPD process unit.

In an embodiment, the feedstock to the hydrodearylation reactor (either whole or fractionated) is mixed with an excess of hydrogen gas in a mixing zone. A portion of the hydrogen gas is mixed with the feedstock to produce a hydrogen-enriched liquid hydrocarbon feedstock. This hydrogen-enriched liquid hydrocarbon feedstock and undissolved hydrogen is supplied to a flashing zone in which at least a portion of undissolved hydrogen is flashed, and the hydrogen is recovered and recycled. The hydrogen-enriched liquid hydrocarbon feedstock from the flashing zone is supplied as a feed stream to the hydrodearylation reactor. The hydrodearylated liquid product stream that is recovered from the hydrodearylation reactor is further processed as provided here.

In certain embodiments, the hydrogen stream is combined with the second product stream before being supplied to the hydrodearylation reactor. In certain embodiments, the hydrogen stream includes a recycled hydrogen stream and a makeup hydrogen stream. In certain embodiments, the hydrogen stream comprises at least 70% hydrogen by weight. The catalyst can be presented as a catalyst bed in the reactor. In certain embodiments, a portion of the hydrogen stream is fed to the catalyst bed in the reactor to quench the catalyst bed. In certain embodiments, the catalyst bed is comprised of two or more catalyst beds. The catalyst can include a support that is at least one member of the group consisting of silica, alumina, titania, and combinations thereof, and further includes an acidic component that is at least one member of the group consisting of amorphous silica-alumina, zeolite, and combinations thereof. The zeolite can be one or more of or derived from FAU, *BEA, MOR, MFI, or MWW framework types, wherein each of these codes correspond to a zeolite structure present in the database of zeolite structures as maintained by the Structure Commission of the International Zeolite Association. In certain embodiments, the catalyst includes an IUPAC Group 8-10 metal and an IUPAC Group 6 metal. In certain embodiments, the catalyst includes an IUPAC Group 8-10 metal that is at least one member of the group consisting of iron, cobalt, and nickel, and combinations thereof. The catalyst includes an IUPAC Group 6 metal that is at least one member of the group consisting of molybdenum and tungsten, and combinations thereof. In certain embodiments, the IUPAC Group 8-10 metal is 2 to 20 percent by weight of the catalyst and the IUPAC Group 6 metal is 1 to 25 percent by weight of the catalyst. In certain embodiments, the catalyst is comprised of nickel, molybdenum, ultrastable Y-type zeolite, and silica-alumina support.

In certain embodiments, the specific reaction conditions include an operating temperature of the reactor during the hydrodearylation reaction that is in the range of 200 to 450° C. In certain embodiments, the specific reaction conditions include an operating temperature of the reactor during the hydrodearylation reaction that is in the range of 250 to 350° C. In certain embodiments, the specific reaction conditions include an operating temperature of the reactor during the hydrodearylation reaction that is in the range of 300 to 350° C. The specific reaction conditions can include a hydrogen partial pressure of the reactor during the hydrodearylation reaction that is in the range of 5 to 100 bar gauge. In certain embodiments, the specific reaction conditions can include a hydrogen partial pressure of the reactor during the hydrodearylation reaction that is in the range of 50 to 100 bar gauge. In certain embodiments, the specific reaction conditions can include a hydrogen partial pressure of the reactor during the hydrodearylation reaction that is in the range of 5 to 80 bar gauge. In certain embodiments, the specific reaction conditions can include a hydrogen partial pressure of the reactor during the hydrodearylation reaction that is in the range of 5 to 30 bar gauge. The hydrogen partial pressure of the reactor during the hydrodearylation reaction can be maintained at less than 20 bar gauge. The specific reaction conditions can include a feed rate of the hydrogen stream that is in the range of 100 to 1000 standard liter per liter of feedstock. The specific reaction conditions can include a feed rate of the hydrogen stream that is in the range of 100 to 300 standard liter per liter of feedstock.

In an embodiment, a system is provided for conversion of alkyl-bridged non-condensed alkyl multi-aromatic compounds to alkyl mono-aromatic compounds. The system includes (i) a first separator that receives a feed stream containing one or more of heavy alkyl aromatic compounds and one or more alkyl-bridged non-condensed alkyl multi-aromatic compounds having at least two benzene rings connected by an alkyl bridge group with at least two carbons and the benzene rings that is connected to different carbons of the alkyl bridge group, and produces a first product stream containing C₉ and C₁₀ compounds and a second product stream containing one or more of heavy alkyl aromatic compounds and alkyl-bridged non-condensed alkyl multi-aromatic compounds; (ii) a hydrodearylation reactor fluidly coupled to the first separator and adapted to receive a hydrogen stream and the second product stream and to produce a third product stream in presence of a catalyst, and the third product stream containing one or more alkyl mono-aromatic compounds; (iii) a second separator fluidly coupled to the hydrodearylation reactor and adapted to receive the third product stream and to produce a benzene-containing stream, a toluene-containing stream, a C₈-rich stream, and a bottoms C₉₊ stream. In certain embodiments, the system further includes a transalkylation unit that is adapted to receive the toluene-containing stream and the bottoms C₉₊ stream and to produce alkyl mono-aromatic compounds. In order to increase the production of benzene and para-xylene, the toluene and C₉ and C₁₀ aromatics are processed within the complex through a toluene, C₉, C₁₀ transalkylation/toluene disproportionation (TA/TDP) process unit to produce benzene and xylenes. Any remaining toluene, C₉, and C₁₀ aromatics are recycled to extinction. In certain embodiments, the second product stream is a C₁₁₊ stream. In certain embodiments, the alkyl mono-aromatic compounds produced by the transalkylation unit includes para-xylene.

A typical refinery with an aromatic complex contains the following units: an atmospheric distillation unit, a diesel hydrotreating unit, an atmospheric residue unit, a naphtha hydrotreating unit, a naphtha reforming unit and an aromatics complex. The whole crude oil is distilled in an atmospheric distillation column to recover a naphtha fraction (compounds with a boiling point ranging from 36° C. to 180° C.), diesel fraction (compounds with a boiling point ranging from 180° C. to 370° C.) and atmospheric residue fraction (compounds with a boiling point at 370° C. or higher). The naphtha fraction is hydrotreated in a naphtha hydrotreating unit to reduce the sulfur and nitrogen content to less than 0.5 part per million by weight and the hydrotreated naphtha fraction is sent to a catalytic reforming unit to improve its quality, such as, an increase in the octane number to produce gasoline blending stream or feedstock for an aromatics recovery unit. Similarly, the diesel fraction is hydrotreated in a separate hydrotreating unit to desulfurize the diesel oil to obtain diesel fraction meeting the stringent specifications of sulfur content that is less than 10 parts per million. The atmospheric residue fraction is either used a fuel oil component or sent to other separation/conversion units to convert low value hydrocarbons to high value products. The reformate fraction from the catalytic reforming unit can be used as gasoline blending component or sent to an aromatic complex to recover high value aromatics, such as, benzene, toluene, and xylenes. The reformate fraction from catalytic reforming unit is split into two fractions: light and heavy reformate. The light reformate is sent to a benzene extraction unit to extract the benzene and recover gasoline that is substantially free of benzene. The heavy reformate stream is sent to a para-xylene (p-xylene) extraction unit to recover p-xylene. Other xylenes that are recovered from the p-xylene unit are sent to a xylene isomerization unit to convert them to p-xylene. The converted fraction is recycled to the p-xylene extraction unit. The heavy fraction from the p-xylene extraction unit is recovered as a process reject or bottoms stream. The aromatics bottoms fraction from an aromatic recovery complex is processed in two ways. One, the aromatics bottoms fraction is fractionated into a 180-° C. fraction (compounds with a boiling point less than 180° C.) and sent to a gasoline pool as blending components, and a 180+° C. fraction sent to a hydrodearylation unit. Alternatively, the aromatics bottoms fraction is sent directly to a hydrodearylation unit to recover light alkyl mono-aromatic compounds from heavy alkyl aromatic and alkyl-bridged non-condensed alkyl aromatic compounds. A typical system for aromatic transalkylation to ethylbenzene and xylenes includes the following components: a first transalkylation reactor, a series of separators, a second transalkylation reactor, a stabilizer, and a p-xylene production unit. The feed stream to the first transalkylation reactor is a mixture of a C₉₊ alkyl aromatics mixture and benzene. This feed stream in brought into contact with a zeolite catalyst in the first transalkylation reactor. The effluent stream from this transalkylation reactor is directed to a separation column. This effluent stream may be combined with effluent streams from the second transalkylation reactor before entry into a separation column. There are three exit streams from the separation column: an overhead stream containing benzene, a bottoms stream of C₈₊ aromatics including ethylbenzene and xylenes, and a side-cut stream containing toluene. The overhead stream is recycled to the first transalkylation reactor. The bottoms stream is supplied to a second separation column. An overhead stream containing ethylbenzene and xylenes from the second separation column is directed to a para-xylene unit to produce a para-xylene product stream and a bottoms stream of C₉₊ alkylaromatics. The side-cut stream from the separation column is recycled to a second transalkylation unit with or without the recovery of toluene. This side-cut stream from the separation column can be combined with bottoms stream from second separation column to form a combined stream that is supplied to a third separation column. This separation column separates the combined stream into a bottoms stream of C₁₁₊ alkylaromatics (“heavies”) and an overhead stream of C₉, C₁₀ alkylaromatics, and lighter compounds (including C₇ alkylaromatics) directed to a second transalkylation unit. Hydrogen is also supplied to the second transalkylation unit. Here, in the second transalkylation unit, the overhead stream and hydrogen are brought in contact with a transalkylation catalyst, and the effluent stream is directed to a stabilizer column. Two streams exit the stabilizer column: an overhead stream of light end hydrocarbons (generally comprising at least ethane) and a bottom stream of a second transalkylation product.

As previously described, the aromatic bottoms stream from an aromatic recovery complex can be directly supplied to a hydrodearylation unit and a hydrodearylated liquid product stream can be recovered for further processing. In an embodiment 100 as described in FIG. 1, the aromatic bottoms stream 104 from an aromatic recovery complex 102 is sent to a separator 106. In an embodiment, this separator 106 can be a separation unit including a distillation column with 5 or more theoretical trays. In an embodiment, the separator 106 can be a flash vessel or a stripper. Two streams exit the separator 106: an overhead stream 108 containing C₉ and C₁₀ compounds and a bottoms stream 110 containing C₁₁₊ compounds. In an embodiment, the overhead stream 108 contains about 50-99 wt. % of the C₉ and C₁₀ compounds. In another embodiment, the overhead stream 108 contains about 60-99 wt. % of the C₉ and C₁₀ compounds. In an embodiment, the overhead stream 108 contains about 80-99 wt. % of the C₉ and C₁₀ compounds. For example, simulated distillation data indicated that the overhead stream 108 contains about 90-99 wt. % of the C₉ and C₁₀ compounds. And this data aligned with the two-dimensional gas chromatography data obtained in this instance, which revealed the stream 104 as containing about 91 wt. % of the C₉ and C₁₀ compounds. The C₉₊ feed from a refinery can be “heavy” with a different composition. In other instances, the C₉ and C₁₀ compounds made up about 68 wt. % of the feed as determined by two-dimensional gas chromatography. The bottoms stream 110 containing C₁₁₊ compounds is directed to a hydrodearylation unit 112 for processing into a hydrodearylated liquid product stream 114. In an embodiment, the bottoms stream 110 contains about 5-99 wt. % of C₁₁₊ compounds. In another embodiment, the bottoms stream 110 contains about 30-99 wt. % of C₁₁₊ compounds. In an embodiment, the bottoms stream 110 contains about 80-99 wt. % of C₁₁₊ compounds. In an embodiment, the hydrodearylated liquid product stream 114 contains greater than 10 wt. % of alkyl mono-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 114 contains greater than 20 wt. % of alkyl mono-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 114 contains greater than 40 wt. % of alkyl mono-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 114 contains about 50 wt. % of alkyl mono-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 114 contains about 70 wt. % of alkyl mono-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 114 contains about 90 wt. % of alkyl mono-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 114 contains less than 70 wt. % of di-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 114 contains less than 50 wt. % of di-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 114 contains less than 40 wt. % of di-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 114 contains less than 20 wt. % of di-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 114 contains less than 10 wt. % of di-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 114 contains less than 1 wt. % of di-aromatic compounds. The overhead stream 108 containing C₉ and C₁₀ compounds is combined with the hydrodearylated liquid product stream 114 leaving the hydrodearylation unit, and this combined stream 116 is supplied to a transalkylation reactor for further processing.

In another embodiment, the aromatic bottoms stream from an aromatic recovery complex is sent to a separator. In an embodiment, this separator can be a separation unit including a distillation column with 5 or more theoretical trays. In an embodiment, the separator can be a flash vessel or a stripper. In an embodiment 200 as described in FIG. 2, the aromatic bottoms stream 204 from an aromatic recovery complex 202 is sent to a first separator 206. Two streams exit the first separator 206: an overhead stream 208 containing C₉ and C₁₀ compounds and a bottoms stream 210 containing C₁₁₊ compounds. In an embodiment, the overhead stream 208 contains about 50-99 wt. % of the C₉ and C₁₀ compounds. In another embodiment, the overhead stream 208 contains about 60-99 wt. % of the C₉ and C₁₀ compounds. In an embodiment, the overhead stream 208 contains about 80-99 wt. % of the C₉ and C₁₀ compounds. In an embodiment, the overhead stream 208 contains about 90-99 wt. % of the C₉ and C₁₀ compounds. The bottoms stream 210 containing C₁₁₊ compounds is directed to a hydrodearylation unit 212 for processing a hydrodearylated liquid product stream 214. In an embodiment, the bottoms stream 210 contains about 5-99 wt. % of C₁₁₊ compounds. In another embodiment, the bottoms stream 210 contains about 30-99 wt. % of C₁₁₊ compounds. In an embodiment, the bottoms stream 210 contains about 80-99 wt. % of C₁₁₊ compounds. The hydrodearylated liquid product stream 214 is supplied to a second separator 216. In an embodiment, the hydrodearylated liquid product stream 214 contains about 10 wt. % of alkyl mono-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 214 contains about 20 wt. % of alkyl mono-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 214 contains about 40 wt. % of alkyl mono-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 214 contains about 50 wt. % of alkyl mono-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 214 contains about 70 wt. % of alkyl mono-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 214 contains about 90 wt. % of alkyl mono-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 214 contains less than 70 wt. % of di-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 214 contains less than 40 wt. % of di-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 214 contains less than 20 wt. % of di-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 214 contains less than 10 wt. % of di-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 214 contains less than 1 wt. % of di-aromatic compounds. The hydrodearylated liquid product stream 214 is supplied to a second separator 216. Four streams exit the second separator 216: a benzene-containing stream 218, a toluene-containing stream 220, a C₈-containing stream 222, and a bottoms C₉₊ stream 224. In an embodiment, the benzene-containing stream 218 contains less than 30 wt. % of benzene. In another embodiment, the benzene-containing stream 218 contains less than 20 wt. % of benzene. In another embodiment, the benzene-containing stream 218 contains less than 10 wt. % of benzene. In another embodiment, the benzene-containing stream 218 contains less than 5 wt. % of benzene. The toluene-containing stream 220 can be directed to a transalkylation reactor as a feed stream. In the transalkylation reactor, the toluene is combined with a C₉₊ stream to produce alkyl mono-aromatic compounds. In an embodiment, the toluene-containing stream 220 contains less than 30 wt. % of toluene. In another embodiment, the toluene-containing stream 220 contains less than 20 wt. % of toluene. In another embodiment, the toluene-containing stream 220 contains less than 15 wt. % of toluene. In another embodiment, the toluene-containing stream 220 contains less than 10 wt. % of toluene. The C₈-containing stream 222 is directed to the p-xylene production unit. In an embodiment, the C₈-containing stream 222 contains less than 30 wt. % of C₈ compounds, such as xylene and ethylbenzene. In another embodiment, the C₈-containing stream 222 contains less than 20 wt. % of these C₈ compounds. In another embodiment, the C₈-containing stream 222 contains less than 10 wt. % of these C₈ compounds. The C₉₊ stream 224 can be supplied as part of a feed stream 226 to a transalkylation unit. In an embodiment, the C₉₊ stream 224 is combined with the overhead stream 208 containing C₉ and C₁₀ compounds and supplied as part of a feed stream 226 to the transalkylation unit.

In an embodiment 300 as described in FIG. 3, the aromatic bottoms stream from an aromatic recovery complex is sent to a first separator 302. Two streams exit the first separator 302: an overhead stream 304 containing C₉ and C₁₀ compounds and a bottoms stream 306 containing C₁₁₊ compounds. In an embodiment, the overhead stream 304 contains about 50-99 wt. % of the C₉ and C₁₀ compounds. In another embodiment, the overhead stream 304 contains about 60-99 wt. % of the C₉ and C₁₀ compounds. In an embodiment, the overhead stream 304 contains about 80-99 wt. % of the C₉ and C₁₀ compounds. For example, simulated distillation data indicated that the overhead stream 304 contains about 90-99 wt. % of the C₉ and C₁₀ compounds.

In an embodiment, the overhead stream 304 containing C₉ and C₁₀ compounds can be supplied as part of a feed stream 320 to a transalkylation unit. The bottoms stream 306 containing C₁₁₊ compounds is directed to a hydrodearylation unit 308 for processing into a hydrodearylated liquid product stream 310. In an embodiment, the bottoms stream 306 contains about 5-99 wt. % of C₁₁₊ compounds. In another embodiment, the bottoms stream 306 contains about 30-99 wt. % of C₁₁₊ compounds. In an embodiment, the bottoms stream 306 contains about 80-99 wt. % of C₁₁₊ compounds. The hydrodearylated liquid product stream 310 is sent to a second separator 312. In an embodiment, the hydrodearylated liquid product stream 310 contains about 10 wt. % of alkyl mono-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 310 contains about 20 wt. % of alkyl mono-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 310 contains about 40 wt. % of alkyl mono-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 310 contains about 50 wt. % of alkyl mono-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 310 contains about 70 wt. % of alkyl mono-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 310 contains about 90 wt. % of alkyl mono-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 310 contains less than 70 wt. % of di-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 310 contains less than 40 wt. % of di-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 310 contains less than 20 wt. % of di-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 310 contains less than 10 wt. % of di-aromatic compounds. In an embodiment, the hydrodearylated liquid product stream 310 contains less than 1 wt. % of di-aromatic compounds.

Four streams exit the second separator 312: a benzene-containing stream 314, a first toluene-containing stream 316, a first C₈-containing stream 318, and a bottoms C₉₊ stream. In an embodiment, the benzene-containing stream 314 contains less than 30 wt. % of benzene. In another embodiment, the benzene-containing stream 314 contains less than 20 wt. % of benzene. In another embodiment, the benzene-containing stream 314 contains less than 10 wt. % of benzene. In another embodiment, the benzene-containing stream 314 contains less than 5 wt. % of benzene. In an embodiment, the first toluene-containing stream 316 contains less than 30 wt. % of toluene. In another embodiment, the first toluene-containing stream 316 contains less than 20 wt. % of toluene. In another embodiment, the first toluene-containing stream 316 contains less than 15 wt. % of toluene. In another embodiment, the first toluene-containing stream 316 contains less than 10 wt. % of toluene.

In an embodiment, the first C₈-containing stream 318 contains less than 30 wt. % of C₈ compounds, such as xylene and ethylbenzene. In another embodiment, the first C₈-containing stream 318 contains less than 20 wt. % of these C₈ compounds. In another embodiment, the first C₈-containing stream 318 contains less than 10 wt. % of these C₈ compounds.

In an embodiment, the bottoms C₉₊ stream is supplied as part of a feed stream 320 to a transalkylation unit. The benzene-containing stream 314 is sent to a third separator 322. Two streams exit the third separator 322: a benzene-enriched stream 324 that is directed to a transalkylation reactor, and a second toluene-containing stream 326 that is directed to a fourth separator 328, either as a separate feed stream or as a mixture with the first toluene-containing stream 316. The first toluene-containing stream 316 can be supplied independently to the fourth separator 328. Two streams exit the fourth separator 328: a toluene-enriched stream 330 that is directed to a transalkylation reactor, and a second C₈-containing stream 332 that is directed to a fifth separator 334, either as a separate feed stream or as a mixture with the first C₈-rich stream 318. The first C₈-rich stream 318 can be supplied independently to the fifth separator 334. Two streams exit the fifth separator 334: a C₈-rich stream 336 that is directed to a p-xylene production unit, and a C₉₊-containing stream 338 that is directed to the transalkylation unit, either as a separate feed stream or as a mixture with the bottoms C₉₊ stream 320. In an embodiment, the C₉₊-containing stream 338 is combined with the overhead stream 304 containing C₉ and C₁₀ compounds from the first separator 302 and supplied as a feed stream 340 to the transalkylation unit. In another embodiment, the overhead stream 304 containing C₉ and C₁₀ compounds from the first separator 302, the bottoms C₉₊ stream 320 from the second separator 312, and the C₉₊-containing stream 338 from the fifth separator 334 are combined and supplied as a feed stream 340 to a transalkylation unit. In another embodiment, each of these streams can be separately supplied to the first transalkylation unit.

Described here is a method and a system used for aromatic transalkylation to ethylbenzene and xylenes. In an embodiment 400 as described in FIG. 4, the aromatic bottoms stream from an aromatic recovery complex is sent to a hydrodearylation unit 402. The hydrodearylated liquid product stream 404, exiting from the hydrodearylation unit 402, may also contain benzene, toluene and C₈ compounds, along with C₉₊ alkyl aromatics. The hydrodearylated liquid product stream 404 is mixed with a benzene-containing stream 406 to form a feed stream 408. The feed stream 408 is supplied to a transalkylation reactor 410 either with or without an additional hydrogen stream 412. The feed stream 408 in the presence of a catalyst is converted to a first product stream 414 containing benzene, C₈₊ aromatics including ethylbenzene and xylenes, and toluene. The first product stream 414 from the transalkylation reactor is directed to a first separation column 416. The first product stream 414 is separated into three fractions: a first overhead stream 418 containing benzene, a first bottoms stream 420 containing C₈₊ aromatics including ethylbenzene and xylenes, and a side-cut stream 422 containing toluene. The first overhead stream 418 is recycled to the first transalkylation unit after benzene is removed via stream 424. The first bottoms stream 420 of C₈₊ aromatics, including ethylbenzene and xylenes, from the first separation column 416 is directed to a second separation column 426. Two streams are recovered from this second separation column 426: a second overhead stream 428 of ethylbenzene and xylenes, which is directed to a para-xylene unit 430 to produce a para-xylene-rich stream 432, and a second bottoms stream 434 of C₉₊ alkylaromatics. The side-cut stream 422 from the first separation column 416 is supplied as part of a feed stream 436 to a third separation column 438 after additional toluene is added or removed (not shown in FIG. 4). Toluene is normally recycled to extinction by reacting with C₉ and C₁₀ to produce benzene and C₈. If there is a decrease or lack of toluene in the system, make-up toluene may be required. If there is a decrease or lack of C₉/C₁₀, the amount of toluene can be proportionately reduced to make the stoichiometry. Certain market conditions may influence the removal of toluene from the system. The side-cut stream 422 is mixed with the second bottoms stream 434 of C₉₊ alkylaromatics to form a combined feed stream 436 that is supplied to the third separation column 438. Two streams are recovered from this third separation column 438: a third bottoms stream 440 of C₁₁₊ alkylaromatics and an overhead stream 442 of C₉ and C₁₀ alkylaromatics and lighter compounds (including C₇ alkylaromatics) directed to the transalkylation reactor 410. In certain embodiments, the unconverted products can be recycled to the hydrodearylation unit 402 (not shown in FIG. 4).

FIG. 5 is a schematic representation of certain components of an aromatics processing system that upgrades fuel oil to a petrochemical feedstock, according to an exemplary embodiment. In an embodiment 500 as described in FIG. 5, the aromatic bottoms stream from an aromatic recovery complex is sent to a hydrodearylation unit 502. The hydrodearylated liquid product stream 504, exiting from the hydrodearylation unit 502, may contain benzene, toluene and C₈ compounds, along with C₉₊ alkyl aromatics. The hydrodearylated liquid product stream 504 is optionally mixed with a benzene-containing stream 506 to form a feed stream 508. In one embodiment, a portion or all of feed stream 508 is supplied to a transalkylation reactor 510 either with or without an additional hydrogen stream 512. In other embodiments, discussed further as follows, all of feed stream 508, or a portion, can be supplied to catalytic dealkylation reactor 511.

The feed stream 508 in the presence of a catalyst in transalkylation reactor 510 is converted to a first product stream 514 containing benzene, C₈₊ aromatics including ethylbenzene and xylenes, and toluene. The first product stream 514 from the transalkylation reactor 510 is directed to a first separation column 516. The first product stream 514 is separated into three fractions: a first overhead stream 518 containing benzene, a first bottoms stream 520 containing C₈₊ aromatics including ethylbenzene and xylenes, and a side-cut stream 522 containing toluene.

Alternatively all, or additionally a portion, of feed stream 508 is supplied to a catalytic dealkylation reactor 511 via feed stream 513 with or without an additional hydrogen stream 517. Catalytic dealkylation reactor 511 allows for the production of additional benzene by dealkylation of alkyl groups disposed on the benzene ring of alkyl aromatic compounds. Catalytic dealkylation reactor 511 can be supplied with feed when maximum benzene production is desired. Product stream 519 of catalytic dealkylation reactor 511 also proceeds to first separation column 516, and benzene production in first overhead stream 518 would be increased and xylene production in first bottoms stream 520 would be decreased compared to the products separated from transalkylation reactor 510. For example, in transalkylation reactor 510 greater than about 95 wt. % benzene can be produced with less than about 5 wt. % xylenes, and in catalytic dealkylation reactor 511 benzene can be produced at greater than about 95 wt. % with alkylated aromatics at below about 5 wt. %, and generally less xylenes.

Optionally, a portion of the overhead stream 518 is recycled to the transalkylation reactor 510 and/or catalytic dealkylation reactor 511 after benzene is removed via stream 524. The first bottoms stream 520 of C₈₊ aromatics, including ethylbenzene and xylenes, from the first separation column 516 is directed to a second separation column 526. Two streams are recovered from this second separation column 526: a second overhead stream 528 of ethylbenzene and xylenes, which is directed to a para-xylene unit 530 to produce a para-xylene-rich stream 532, and a second bottoms stream 534 of C₉₊ alkylaromatics.

The side-cut stream 522 from the first separation column 516 is supplied as part of a feed stream 536 to a third separation column 538 after additional toluene is added or removed (not shown in FIG. 5). Toluene is normally recycled to extinction by reacting with C₉ and C₁₀ to produce benzene and C₈. If there is a decrease or lack of toluene in the system, make-up toluene may be required. If there is a decrease or lack of C₉/C₁₀, the amount of toluene can be proportionately reduced to make the stoichiometry. Certain market conditions may influence the removal of toluene from the system. The side-cut stream 522 is mixed with the second bottoms stream 534 of C₉₊ alkylaromatics to form a combined feed stream 536 that is supplied to the third separation column 538. Two streams are recovered from this third separation column 538: a third bottoms stream 540 of C₁₁₊ alkylaromatics and an overhead stream 542 of C₉ and C₁₀ alkylaromatics and lighter compounds (including C₇ alkylaromatics) directed to the transalkylation reactor 510 and/or the catalytic dealkylation reactor 511. In certain embodiments, the unconverted products can be recycled to the hydrodearylation unit 502 (not shown in FIG. 5).

As shown in FIG. 5, transalkylation reactor 510 and catalytic dealkylation reactor 511 are separate units; however, in other embodiments one unit can be designed with flexible catalysts and operating conditions to carry out either transalkylation or dealkylation at appropriately chosen operating conditions and depending on demand for benzene versus xylenes. Suitable transalkylation catalysts include, but are not limited to a Beta zeolite at a molar silica-to-alumina (SAR) ratio of about 25, or between about 10 and about 200, (optionally with a Rhenium (Re) metal content of about 0.5 wt. %); an IMF zeolite at a SAR of about 24, or between about 15 and about 35, (optionally with a Re metal content of about 0.25 wt. %); an ITH zeolite at a SAR of about 100, or between about 30 and about 200; an MFI zeolite at a SAR of about 35, or between about 25 and about 200 (optionally with a Re metal content of about 0.5 wt. %); an MOR zeolite at a SAR of about 20, or between about 10 and about 200, or about 96, or about 33.5 (optionally with a Re metal content of between about 0.29 wt. % and 0.5 wt. %); an MWW zeolite at a SAR of about 33, or between about 30 and about 200; an NES zeolite at a SAR of about 67 or about 60, or between about 30 and about 100; and a TUN zeolite with an SAR of about 40, or between about 15 and about 100. Disproportionation of ethylbenzene, for example, can be achieved over acidic forms of different structural types of zeolites including ZSM-5 (MFI framework), MOR, *BEA (Beta zeolite), Zeolite Y (FAU framework), MCM-22 (MWW framework), MCM-40 (aluminophosphate) and their modified impregnated forms.

Operating conditions in a transalkylation unit and catalytic dealkylation unit can overlap, but can be controlled to increase benzene production in the catalytic dealkylation unit if desired. A transalkylation reaction can be favored at a temperature between about 400° C. to about 450° C. or 460° C., at a pressure between about 25 to about 35 bars, at a feed liquid hourly space velocity (LHSV) of between about 1 to about 3 h⁻¹, with catalyst active phase metals such as noble metals (for example, platinum and palladium), rare earth metals, or combinations thereof, without steam, and under hydrogen addition. A suitable transalkylation unit can also be operated at about 300° C. and about 1 atm.

A dealkylation reaction can be favored at a temperature between about 200° C. to about 500° C., at a pressure between about 10 to about 50 bars, at a feed LHSV of between about 1 to about 3 h⁻¹, with catalyst active phase metals such as chromium and its oxides, molybdenum and its oxides, platinum and its oxides, or combinations thereof, without steam, and under hydrogen addition. Additional suitable hydrodealkylation catalysts include Group VI or Group VIII catalysts having Bronsted acidity, for example alumina. These can be bi-metallic catalysts. Supported Ni catalysts are also suitable. One example is Pt/H-ZSM-5 for dealkylation of C₉₊ aromatics. Catalysts for transalkylation are generally zeolitic, while catalysts for catalytic dealkylation are zeolitic, amorphous, or both.

Described here are processes and systems to fractionate the reject/bottoms stream of a xylene re-run column and to upgrade the fuel oil components (heavy fraction) to petrochemical feedstock. Also described are embodiments to upgrade the as-received reject/bottoms stream from the xylene re-run column. The C₉₊ stream from a xylene re-run column is fractionated to remove C₉ and C₁₀, leaving a C₁₁₊ stream, which is considered as a low-value fuel oil stream. The C₉ and C₁₀ stream is directed to a TA/TDP process unit to be processed to yield increased quantities of C₈ that can be further processed downstream to yield para-xylene. The C₁₁₊ fuel oil stream is subjected to hydrodearylation. The unconverted C₁₁₊ (mainly condensed diaromatics) stream is directed as fuel oil (approximately 25 wt. % of the original fuel oil stream). The methods and systems disclosed here allow a low-value fuel oil stream to be upgraded into petrochemical feedstock. Approximately 75% of the fuel oil is converted to isomer grade mixed xylenes.

EXAMPLES

A couple of methods and systems for integration of a hydrodearylation process with a transalkylation process are illustrated here. While the particular example provided below is for a stream containing C₉₊ compounds, the methods and systems for integration of a hydrodearylation process with a transalkylation process can utilize a C₁₁₊ feed.

Example 1

About 7.97 kilograms of an aromatic bottoms fraction, derived from a non-fractionated C₉₊ feed, was distilled using a lab-scale true boiling point distillation column with 15 or more theoretical plate using the ASTM D2892 method. The feed stream contains about 83 weight percent (wt. %) of a gasoline fraction (compounds with a boiling point ranging from 36° C. to 180° C.) and about 17 wt. % of a residue fraction (compounds with a boiling point above 180° C.).

Properties and composition of the feed stream are shown in Tables 1 and 2.

TABLE 1 Feedstock Aromatics Gasoline Residue Property Bottoms Fraction Fraction Density 0.8834 0.8762 0.9181 Octane Number Not applicable 108 Not applicable ASTM D2799

TABLE 2 Boiling Point, ° C. Boiling Point, (Feedstock ° C. Aromatics (Gasoline Boiling Point, ° C. Property Bottoms) Fraction) (Residue Fraction) Initial Boiling 153 154 163 Point 10 wt. % 163 164 190 30 wt. % 166 166 202 50 wt. % 172 171 231 70 wt. % 175 174 289 90 wt. % 191 183 324 Final Boiling 337 204 359 point

In an example of a hydrodearylation process, a feedstock consisting of a non-fractionated xylene rerun column bottoms stream with the above described properties was treated in a hydrodearylation reaction zone containing a catalyst having nickel and molybdenum with ultrastable Y-type (USY) zeolite on a silica-alumina support operated at hydrodearylation conditions including a temperature ranging from 280 to 340° C., at a hydrogen partial pressure of 15 or 30 bar, a liquid hourly space velocity of 1.7 hr⁻¹. Feed and hydrodearylated liquid product compositions, as analyzed by two-dimensional gas chromatography, are provided in Table 3.

TABLE 3 Run Temperature Pressure MA NMA MN DN P NDA DA TrA # ° C. Bar Wt. % Wt. % Wt. % Wt. % Wt. % Wt. % Wt. % Wt. % Feed 0 0 92.28 1.82 0.15 0.12 0.37 0.59 4.34 0.33 1 340 30 91.67 2.91 2.1 0.43 0.94 0.43 1.38 0.15 3 320 30 92.95 3.04 1.56 0.33 0.37 0.45 1.16 0.13 5 300 30 92.98 3.13 1.33 0.29 0.34 0.51 1.3 0.13 7 280 30 93.2 3.1 0.95 0.23 0.3 0.54 1.55 0.14 15 340 15 93.47 2.38 0.46 0.17 0.55 0.59 2.13 0.26 17 320 15 93.69 2.15 0.34 0.1 0.4 0.72 2.34 0.26 19 300 15 93.73 2.1 0.29 0.08 0.35 0.71 2.46 0.29 21 280 15 93.63 2.09 0.27 0.08 0.33 0.77 2.54 0.28 Key for Table 2—MA: Mono Aromatics; NMA: Naphtheno Mono Aromatics; MN: Mono-Naphthenes; DN: Di-naphthenes; P: Paraffins; NDA: Naphtheno Di Aromatics; DA: Diaromatics; and TrA: Tri Aromatics

For example, subjecting the feed to hydrodearylation conditions in the presence of the catalyst and hydrogen at 320° C. and 30 bar, there is an approximately 75% reduction in diaromatic content. The decrease in the diaromatic content demonstrates that hydrodearylation has occurred and the low-value heavy components of the stream have been upgraded to higher value components. The technology also takes a low-value fuel oil from an aromatic bottoms/reject stream from an aromatic complex and upgrades the fuel oil to petrochemical feedstock.

Ranges may be expressed herein as from about one particular value and to about another particular value. When such a range is expressed, it is to be understood that another embodiment is from the one particular value and/or to the other particular value, along with all combinations within said range. Where the range of values is described or referenced here, the interval encompasses each intervening value between the upper limit and the lower limit as well as the upper limit and the lower limit and includes smaller ranges of the interval subject to any specific exclusion provided. Where a method comprising two or more defined steps is recited or referenced herein, the defined steps can be carried out in any order or simultaneously except where the context excludes that possibility. While various embodiments have been described in detail for the purpose of illustration, they are not to be construed as limiting, but are intended to cover all the changes and modifications within the spirit and scope thereof. 

What is claimed is:
 1. A process for recovery of alkyl mono-aromatic compounds and benzene, the process comprising the steps of: supplying an aromatic bottoms stream comprising C₁₁₊ aromatic compounds from an aromatic recovery complex to a hydrodearylation reactor with a hydrodearylation catalyst; producing from the hydrodearylation reactor by processing the C₁₁₊ aromatic compounds under hydrodearylation conditions a hydrodearylated liquid product stream comprising benzene, toluene, and C₈₊ compounds; supplying a portion of the hydrodearylated liquid product stream to a transalkylation reactor to react the hydrodearylated liquid product stream in the presence of a transalkylation catalyst to produce a transalkylation product stream including benzene, C₈₊ aromatics including ethylbenzene and xylenes, and toluene; separating in a first separation column the transalkylation product stream into three fractions including a first overhead stream comprising benzene, a first bottoms stream comprising C₈₊ aromatics including ethylbenzene and xylenes, and a side-cut stream comprising toluene; recycling toluene from the side-cut stream comprising toluene to the transalkylation reactor; and producing para-xylene from the first bottoms stream comprising C₈₊ aromatics including ethylbenzene and xylenes.
 2. The process of claim 1, wherein the aromatic bottoms stream is from a xylene rerun column of the aromatic recovery complex.
 3. The process of claim 1, further comprising the step of supplying a hydrogen feed stream to the transalkylation reactor.
 4. The process of claim 1, further comprising the step of supplying a hydrogen feed stream to the hydrodearylation reactor.
 5. The process of claim 4, wherein a portion of the hydrogen feed stream is supplied to a catalyst bed in the hydrodearylation reactor to quench the catalyst bed.
 6. The process of claim 1, wherein the hydrodearylation catalyst includes a support being at least one member of the group consisting of silica, alumina, titania, and combinations thereof, and further includes an acidic component being at least one member of the group consisting of amorphous silica-alumina, alumina, zeolite, and combinations thereof.
 7. The process of claim 6, wherein the zeolite is one or more of or derived from FAU, *BEA, MOR, MFI, or MWW framework types.
 8. The process of claim 1, wherein the hydrodearylation catalyst includes an IUPAC Group 6-10 metal being at least one member of the group consisting of iron, cobalt, nickel, molybdenum, tungsten, and combinations thereof.
 9. The process of claim 8, wherein the wherein the IUPAC Group 8-10 metal is 2 to 20 percent by weight of the hydrodearylation catalyst and the IUPAC Group 6 metal is 1 to 25 percent by weight of the catalyst.
 10. The process of claim 1, wherein conditions in the hydrodearylation reactor include an operating temperature in the range of about 200 to 450° C.
 11. The process of claim 1, wherein conditions in the hydrodearylation reactor include an operating temperature in the range of about 250 to 450° C.
 12. The process of claim 1, wherein conditions in the hydrodearylation reactor include an operating hydrogen partial pressure in the range of about 5 bar gauge to 100 bar gauge.
 13. The process of claim 1, further comprising the step of supplying a portion of the hydrodearylated liquid product stream to a catalytic dealkylation reactor comprising a dealkylation catalyst to produce a catalytic dealkylation product stream including benzene, wherein benzene content in the catalytic dealkylation product stream is greater than the benzene content in the transalkylation product stream.
 14. The process of claim 13, further comprising the step of supplying the catalytic dealkylation product stream to the first separation column.
 15. The process of claim 13, where the transalkylation catalyst and dealkylation catalyst each comprises a zeolite.
 16. The process of claim 15, where the transalkylation catalyst comprises at least one catalyst selected from the group consisting of: Beta zeolite; IMF zeolite; ITH zeolite; MFI zeolite; MOR zeolite; MWW zeolite; NES zeolite; Rhenium metal; and a TUN zeolite.
 17. The process of claim 1, where the transalkylation reactor operates at a temperature between about 400° C. to about 450° C., at a pressure between about 25 to about 35 bars, at a feed liquid hourly space velocity (LHSV) of between about 1 to about 3 h⁻¹, with at least one catalyst active phase metal including a noble metal or a rare earth metal, without steam, and under hydrogen addition.
 18. The process of claim 13, where the catalytic dealkylation reactor operates at a temperature between about 200° C. to about 500° C., at a pressure between about 10 to about 50 bars, at a feed LHSV of between about 1 to about 3 h⁻¹, with at least one catalyst active phase metal selected from the group consisting of chromium and its oxides, molybdenum and its oxides, platinum and its oxides, without steam, and under hydrogen addition.
 19. The process of claim 13, further comprising the step of recycling toluene from the side-cut stream comprising toluene to the catalytic dealkylation reactor. 